WO2015135968A1 - Catalyseur contenant de l'yttrium pour l'hydrogénation du dioxyde de carbone à haute température, l'hydrogénation du dioxyde de carbone à haute température et le reformage combinés et/ou le reformage ainsi qu'un procédé d'hydrogénation du dioxyde de carbone à haute température, d'hydrogénation du dioxyde de carbone à haute température et de reformage combinés et/ou de reformage - Google Patents

Catalyseur contenant de l'yttrium pour l'hydrogénation du dioxyde de carbone à haute température, l'hydrogénation du dioxyde de carbone à haute température et le reformage combinés et/ou le reformage ainsi qu'un procédé d'hydrogénation du dioxyde de carbone à haute température, d'hydrogénation du dioxyde de carbone à haute température et de reformage combinés et/ou de reformage Download PDF

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Publication number
WO2015135968A1
WO2015135968A1 PCT/EP2015/055022 EP2015055022W WO2015135968A1 WO 2015135968 A1 WO2015135968 A1 WO 2015135968A1 EP 2015055022 W EP2015055022 W EP 2015055022W WO 2015135968 A1 WO2015135968 A1 WO 2015135968A1
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WIPO (PCT)
Prior art keywords
catalyst
carbon dioxide
reforming
yttrium
range
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PCT/EP2015/055022
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German (de)
English (en)
Inventor
Stephan A. Schunk
Ekkehard Schwab
Andrian Milanov
Guido WASSERSCHAFF
Thomas Roussiere
Andreas Strasser
Carlos LIZANDARA
Robert Müller
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Basf Se
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Application filed by Basf Se filed Critical Basf Se
Priority to RU2016140372A priority Critical patent/RU2016140372A/ru
Priority to JP2016557232A priority patent/JP2017507779A/ja
Priority to KR1020167028074A priority patent/KR20160133490A/ko
Priority to CN201580013170.6A priority patent/CN106102905A/zh
Priority to US15/126,217 priority patent/US20170080407A1/en
Priority to EP15708833.7A priority patent/EP3116826B1/fr
Priority to CA2942587A priority patent/CA2942587A1/fr
Publication of WO2015135968A1 publication Critical patent/WO2015135968A1/fr

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    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
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    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
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Definitions

  • Yttrium-containing catalyst for high temperature carbon dioxide hydrogenation for high temperature carbon dioxide hydrogenation, combined high temperature carbon dioxide hydrogenation and reforming and / or reforming, and a process for high temperature carbon dioxide hydrogenation, combined high temperature carbon dioxide hydrogenation and reforming and / or reforming
  • the invention relates to a process for the preparation of a catalyst for the high-temperature process (i) carbon dioxide hydrogenation, (ii) combined high-temperature carbon dioxide hydrogenation and reforming and / or (iii) reforming of hydrocarbon-containing compounds and / or carbon dioxide and the use of the catalyst according to the invention in conjunction with the reforming and / or hydrogenation of hydrocarbons, preferably CH 4 , in the presence of CO2.
  • an aluminum source which preferably comprises a water-soluble precursor source, is contacted with a yttrium-containing metal salt solution, dried and calcined.
  • the metal salt solution has at least one element from the group Co, Cu, Ni, Fe, Zn.
  • cobalt-containing catalyst systems for the catalytic partial oxidation of methane for the production of synthesis gas. It is disclosed that cobalt metal or a cobalt-containing component may co-exist with a carrier, wherein the cobalt is not structurally incorporated into the carrier. In a list that a variety of support materials is also called Yttriumaluminiumgarnet. In particular, the inventors include in their invention that in the partial oxidation of methane with oxygen, reactions such as the dry reforming of methane with carbon dioxide can take place.
  • nickel-modified hexaaluminates for the reforming of methane and carbon dioxide to synthesis gas are described, for example, in a publication by Zlin Xu et al. (Zhalin Xu, Ming Zhen, Yingli Bi Kaiji Zhen, Applied Catalysis A: General 198 (2000) pp. 267-273).
  • Zlin Xu et al. Zhalin Xu, Ming Zhen, Yingli Bi Kaiji Zhen, Applied Catalysis A: General 198 (2000) pp. 267-273.
  • the nickel-modified hexaaluminates have greater activity and better stability than the conventional nickel-containing catalysts where the nickel was deposited on the support materials.
  • an oxidation catalyst comprising metal-exchanged hexaaluminates.
  • the catalyst has good catalytic activity and stability at high temperatures, and the activity is maintained over a longer period of time.
  • the catalysts have a suitability as oxidation catalysts.
  • the catalysts are suitable for the treatment of gases from methane combustion, wherein in particular the use in turbines is of importance, with Natural gas to be operated.
  • the synthesis of the hexaaluminate-containing catalysts is based on the use of boehmite particles.
  • the hexaaluminates disclosed in US Pat. No. 7,442,669 B2 contain up to three different metal species from groups Mi, IVb and M3.
  • the group Mi comprises elements from the group of rare earth elements
  • the group M2 comprises elements from the group of alkaline earth elements
  • the group M3 comprises elements from the group of transition metals, wherein Mn, Fe, Co, Ni, Cu, Ag, Au, Rh , Ru, Pd, Ir and Pt.
  • To characterize the catalysts they were tested for methane replacement activity, with the catalysts exposed to a gas stream containing 3% by volume of methane. The tests were at a pressure of 5 and performed a GHSV of 17,000 hr. 1 As a measure of the efficiency of the catalysts, the temperature T1 / 2 required to convert fifty percent of the methane was determined.
  • the tested catalysts were subjected to different aging protocols before the catalytic tests.
  • EP 2,119,671 discloses the synthesis of hexaaluminate-containing catalysts in the presence of template materials.
  • the template materials are an advantage. They influence the formation of certain pore structures. In the hexaaluminates prepared by the process according to the invention, the pore structure can thus be controlled.
  • S. Nugroho et al. the production of pure phase barium hexa-aluminate, which was obtained by tempering barium oxide and aluminum oxide (ie BaO and Al 2 O 3) by means of a solid state reaction at temperatures of 1450 ° C.
  • barium oxide and aluminum oxide ie BaO and Al 2 O 3
  • p. 466- M. Machida et al. disclose the preparation of phase pure barium hexaaluminates obtained by the hydrolysis of the corresponding alkoxides, which are treated at temperatures up to 1300 ° C.
  • the resulting hexaaluminate phases have surface areas of 1 1 m 2 / g.
  • F. Yin et al. for the production of hexaaluminates by means of the combustion of urea (ie the so-called urea combustion method), which differs from other disclosures in that the thermal treatment of the starting materials takes place at a much lower temperature than in the otherwise known methods.
  • F. Yin et al. indicate that the phase pure hexaaluminate material was already obtained at 500 ° C. The material obtained had a surface area of 20 m 2 / g.
  • Hexaaluminates disclosed which may contain different cations, including lanthanum-containing hexaamluminates, which may contain different divalent cations such as Mg, Ca, Ni, Co, Zn and Fe.
  • different processes are disclosed, which differ from one another in each case with regard to the mixing steps used and the thermal treatment steps.
  • the catalysts according to the invention all of which are doped with rhodium as the active metal, are used in a process for the partial oxidation of gasoline in the presence of oxygen, which serves to produce a hydrogen-rich gas mixture. Temperatures in the range of 1000 ° C and higher may occur in the partial oxidation reactions used to reform fuels, and because of the high temperatures, it is necessary to develop particularly sinter resistant catalysts for this purpose.
  • Todd H. Gardner deals with the use of hexaaluminates as catalysts for the partial oxidation of fuels obtained in the middle fraction distillation.
  • lanthanum-containing, barium-containing and strontium-containing hexaaluminates are described, which contain different transition metal cations. may contain.
  • the focus of this work is the investigation of hexaalimi- lates containing nickel, cobalt or iron, where the transition metals are present in different proportions and are combined with the cations from the group Sr, La or Ba, which are also present in different proportions.
  • the work is directed specifically to an investigation of pure-phase hexaaluminates.
  • the catalysts were used for the partial oxidation of n-tetradecane.
  • the partial oxidations were carried out at a pressure of about 2 bar, a GHSV of 50,000 r 1 and using an oxygen to carbon ratio (ie, O to C) of 1, 2.
  • CN 101306361 A discloses hexaaluminates which are used as catalysts for carrying out reactions for the oxidation of hydrocarbons.
  • the hexaaluminates have the cationic species La, Ba or Ca, and as transition metal cations, the hexaaluminates may have Cr, Mn, Fe, Co, Ni or Cu.
  • US 20070149392 discloses the use of a multi-component catalyst for an RWGS reaction.
  • active metals lead copper and / or zinc oxide are described on support materials, also platinum on ceria and supported gold.
  • the reaction temperature of the RWGS is 400 ° C.
  • WO 2001/17674 describes the use of supported copper / zinc catalysts for the RWGS reaction.
  • the operating temperature of these catalysts is in the range of 150-300 ° C.
  • EP 725 038 describes the use of multicomponent catalysts containing Group VIII and Via metals supported on zinc oxide in combination with a Group IIIb and IVa metal. The use of such active materials up to temperatures of up to 600 ° C for conversion tion of educt gases of the composition hydrogen to carbon dioxide of 1 is described.
  • EP 601 956 describes the use of commercially available reforming catalysts with the active metals nickel, iron, copper and zinc. The materials are described as advantageous for use at temperatures of 400 to 800 ° C and educt gases of the composition hydrogen to carbon dioxide from 1, 5 to 6.5.
  • EP 291 857 describes the use of a nickel-based catalyst for the RWGS.
  • the catalyst consists of an alumina-containing carrier material. The use of the catalyst is described as being advantageous for the combined reforming and RWGS reaction.
  • supported catalysts are used as catalysts in reforming reactions in the prior art.
  • a carrier material is impregnated with a precursor solution by a suitable impregnation process and transferred to the active catalyst by subsequent thermal and physicochemical treatment steps (Alvin B. Stiles, Catalyst Manufacture, CRC Press 1995).
  • the support is intended to produce an intimate contact of the active metal with the surface of the support and, by suitable treatment, to produce a high dispersion of the active metal.
  • This approach is often disadvantageous because the resulting small metal particles often have a high tendency to sinter and the contact of oxide and metal nanoparticles produced by the support often does not lead to the desired intimacy.
  • One of the objects underlying the invention is to provide an improved catalyst, in particular, the catalyst should have improved activity and / or resistance to coke buildup, and its use in an improved process, in particular at temperatures of 600 ° C. up to 1400 ° C and loads of 5000 to 100000 h-1, for high temperature carbon dioxide hydrogenation, for combined high temperature carbon dioxide hydrogenation and reforming and / or reforming.
  • the production process of these catalysts should be as energy efficient and resource efficient.
  • the process should be suitable for high-temperature carbon dioxide hydrogenation, combined high-temperature carbon dioxide hydrogenation and reforming and / or reforming syngas production.
  • Another task is also that the invention Permitted method for high temperature carbon dioxide hydrogenation, combined high temperature carbon dioxide hydrogenation and reforming and / or reforming, in particular for the combined high temperature carbon dioxide hydrogenation and reforming of hydrocarbons, in the presence of methane.
  • Another object within the scope of the invention is to identify particularly active catalysts which, even at high loads, in particular greater than 10,000 h-1, are still able to convert a reactant gas mixture into a composition which is close to the thermodynamically predicted equilibrium , Particularly active catalysts make it possible to make the reactor smaller and thus keep the investment for this part of the plant small.
  • a catalyst or catalyst precursor advantageously high-temperature carbon dioxide hydrogenation, for the combined high-temperature carbon dioxide hydrogenation and reforming and / or reforming, which is characterized in that it comprises at least one crystalline material Yttrium and aluminum, which is characteristic of the crystalline material, has at least one of the following structures from the group cubic garnet structure, thorathic perovskite structure, hexagonal perovskite structure and / or monoclinic perovskite structure (ie Y.sub.4Al.sub.2O.sub.9), where the catalyst is Cu, Fe, Co, Zn and / or Ni, in particular Cu, Fe, Co and / or Ni contains.
  • high temperature process processes at temperatures of> 600 ° C, in particular> 600 ° C and ⁇ 1400 ° C.
  • the metal species Cu, Fe, Co, Zn and / or Ni are preferably present within the crystalline material as substituents of Y and / or Al.
  • the metal species Cu, Fe, Co, Zn and / or Ni may be either (i) within the crystalline material as substituents of Y and / or Al or (ii) may be present on the surface of the catalyst in zerovalent form. In the case of variant (ii), Cu, Fe, Zn and / or Ni are preferred. If the metal species Cu, Fe, Co, Zn and / or Ni, preferably Cu, Fe, Zn and / or Ni, are present on the surface of the catalyst, these are preferably present as X-ray amorphous nanoparticles.
  • the catalyst of the present invention is preferably used for combined high temperature carbon dioxide hydrogenation and reforming of hydrocarbons in the presence of methane.
  • the following wt .-% and mol .-% refer in each case to the entire catalyst or catalyst precursor; whereby the balance area is closed over the metals.
  • the catalyst according to the invention is characterized in that it has a Y content in the range of 15-80 mol%, preferably 17-70 mol%, more preferably in the range of 20-70 mol%.
  • the catalyst according to the invention is characterized in that it has an Al content in a range from 10 to 90 mol%, preferably 20 to 85 mol% and more preferably in the range from 30 to 80 mol%.
  • the catalyst according to the invention is characterized in that the content of the at least one further element from the group Zn, Cu, Ni, Co, Fe, or the sum of several of these elements, in a range of 0, 01 to 10 mol%, preferably 0.02 to 7 mol%, more preferably 0.1 to 5 mol%.
  • the sum of Y and Al is greater than 80 mole%, more preferably greater than 90 mole%, and most preferably greater than 95 mole%; preferably, the sum of Y and Al is in a range of 80 to 99.99 mol%.
  • the catalyst or catalyst precursor according to the invention for high-temperature carbon dioxide hydrogenation, combined high-temperature carbon dioxide hydrogenation and reforming and / or reforming comprises at least one crystalline material containing at least yttrium, aluminum and oxygen species and the at least one component with cubic garnet structure, orthorhombic perovskite structure, hexagonal Perovskite structure and / or monoclinic perovskite structure, wherein at least a portion of the yttrium and / or aluminum species within the crystalline material are substituted by at least one species selected from the group consisting of Cu, Ni, Co, Fe, Zn. Substitution may be by either one of Cu, Ni, Co, Fe, Zn, and by two, three, four, or five of said species of this group.
  • Preferred combinations are Cu with Zn, Ni with Zn, Co with Zn, Co with Ni, Cu with Ni and / or Cu with Co.
  • the main phases of (i) Y3AI5O12 (YAG) with cubic yttrium-aluminum-Garnet structure, ( ii) YAIO3 (YAP) with orthorhombic and / or hexagonal yttrium aluminum perovskite structure and / or (iii) Y4AI2O9 (YAM) with monoclinic perovskite structure of the catalyst according to the invention advantageously have a weight greater than 51% by weight, preferably greater than 70% by weight, in particular greater than 80% by weight, very particularly preferably greater than 90% by weight, more preferably greater than 95% by weight, more preferably greater than 97% by weight.
  • the catalyst or catalyst precursor according to the invention can be composed of (i) Y3AI5O12 (YAG) with cubic yttrium aluminum Garnet structure, (ii) YAIO3 (YAP) with orthorhombic and / or hexagonal yttrium aluminum perovskite structure and / or (iii) Y 4 Al 2 O 9 (YAM) having a monoclinic perovskite structure, which are preferably present in a range of 51 to 100% by weight, more preferably 60 to 99% by weight, most preferably 70 to 97% by weight, at least also contain a secondary phase, whereby the proportion of at least one secondary phase in the range 0-49 wt .-% (with respect to the structurally detectable balance space), preferably in the range of 1 - 40 wt .-%, more preferably in the range of 3 - 30 wt .-%.
  • the at least one secondary phase may, for example, be oxides which contain Cu, Zn, Ni, Co and / or Fe and / or oxides of yttrium.
  • the minor phases are selected from the group alpha-alumina, theta-alumina, YCUO3, YC0O3, YN1O3, cobalt-, iron-, copper-, zinc-, nickel- and yttrium-containing Ruddelson-Popper phases, YFeO3, CuAl2O3, C0Al2O4, N1Al2O4, FeA04, yttrium-stabilized alumina and / or yttrium-stabilized alumina hydroxide, with the yttrium-containing secondary phases being preferred.
  • a catalyst or catalyst precursor whose BET surface area is greater than 2 m 2 / g, more preferably greater than 4 m 2 / g, even more preferably greater than 8 m 2 / g and particularly preferably greater than 15 m 2 / G.
  • the catalyst or catalyst precursor according to the invention is characterized in that contains at least yttrium aluminum garnet as the main phase.
  • a comparison of the composition of the catalyst according to the invention containing yttrium aluminum yarn with a material consisting entirely of yttrium and aluminum and having a well-formed YAG structure Y3Al5O12 (YAG) shows that the catalyst according to the invention comprises the catalytically active elements Cu, Ni, Co, Zn and / or Fe, preferably in isomorphous substitution, has in the YAG lattice.
  • An explanation of the formation of the catalyst according to the invention is that the zinc, copper, nickel, iron and / or Kobalt Anlagenn species added to the synthesis system almost completely, ie preferably greater than 70 wt .-%, in particular greater than 80 wt .-%, most preferably greater than 95 wt .-%, more preferably greater than 97 wt .-% are incorporated into the structure of the Garnet and hardly for the formation of the secondary phases, preferably no zinc, copper, nickel, iron and / or cobalt is more available.
  • the formation of secondary phases is suppressed and the formation of the target phases of the invention from the aluminum- and yttrium-containing species takes place.
  • aluminates, spinels or perovskites of the elements Zn, Cu, Ni, Co and / or Fe or other phases of the elements Y, Zn, Cu, Ni, Co, Fe and / or Al which are known to the person skilled in the art is preferably less than 15% by weight, in particular less than 10% by weight, very particularly preferably less than 5% by weight; Ideally, this education is completely avoided.
  • the above explanation is not intended to limit the invention in any way.
  • the catalyst or catalyst precursor comprises at least one noble metal-containing promoter from the group Pt, Rh, Ru, Pd, Ir, Au, wherein the proportion of noble metal-containing promoters in the range of 0.001 to 5 mol% with respect to the catalyst, preferably in the range of 0.1 to 3 mol%.
  • the catalyst or catalyst precursor may also comprise a proportion, preferably less than 15 mol%, in particular less than 10 mol%, very particularly preferably less than 5 mol%, of further cation species (hereinafter cation species I) which are preferably selected from the group of rare earths, with rare earths such as Ce, La, Pr, Tb, Nd, Eu are particularly preferred.
  • cation species I further cation species
  • the catalyst or catalyst precursor may also comprise a proportion, preferably less than 3 mol%, in particular less than 1 mol%, very particularly preferably less than 0.5 mol%, of further cation species (hereinafter cation species II) , which are preferably selected from the group Mg, Ca, Sr, Ba, Ga, Be, Cr, Mn.
  • cation species II further cation species
  • garnet and garnet are considered synonymous denominations.
  • step (ii) contacting the aluminum source, with a yttrium-containing compound and at least one further metal salt of the group copper, zinc, nickel, cobalt or iron, (iii) intimately mixing the aluminum source from step (i) with the substances from step (ii),
  • the components in the mixing in step (iii) are not in the form of the dissolved metal salts but in the form of a melt
  • the components can also be added without a solvent.
  • a precipitant may also be added to the dissolved components. Suitable precipitants include soluble carbonates such as sodium carbonate or sodium bicarbonate, aqueous ammonia solution and / or soluble hydroxides such as sodium or potassium hydroxide, and mixtures thereof. gene enumerated and other known to those skilled basic precipitant.
  • the precipitant is added as an aqueous solution. Particularly included within the scope of the invention are precipitation processes in which the temperature and pH are controlled and / or controlled during the precipitation.
  • Preferred is a pH in the range of 6.5-13, more preferably 7.5-12.
  • those processes are included where the precipitation takes place at a pH greater than 7.5 and which is kept constant, and at a temperature which is above 20 ° C, preferably above 25 ° C.
  • treatment steps for washing the precipitated material are also included in the preparation process according to the invention.
  • the aluminum source is selected from the group of highly reactive aluminas and hydroxides.
  • the aluminum source contains dispersible primary particles, with a primary particle size of less than or equal to 500 nm being preferred.
  • alcoholates include alcoholates, carboxylic acid salts, organometallic compounds or complex compounds of the starting compounds of the invention of Al, Y, Ni, Co, Fe, Ce, La, Cu, Ga, Zn.
  • the aluminum source is used as an aqueous dispersion having an acidic or basic pH.
  • aqueous dispersion having an acidic or basic pH is particularly preferred.
  • basic solutions or dispersions with polyaluminum chloride is a product, which is led by the company BK Giulini under the trade name Giufloc.
  • One aspect of the invention also relates to the process for the preparation of the catalyst.
  • the term catalyst or catalyst precursor according to the invention comprises yttrium-containing materials which are characterized by a high proportion of YAG phase.
  • YAG phase includes phases which are (i) Y3Al5O12 (YAG) with cubic yttrium aluminum Garnet structure, (ii) YAIO3 (YAP) with orthorhombic and / or hexagonal yttrium
  • the catalyst contains secondary phases, the proportion of secondary phase is preferably in the range from 0 to 49 wt.%, More preferably in the range from 1 to 40 wt.% And even more preferably in the range from 3 to 30 wt.
  • it is YAIO3 (YAP) having orthorhombic or hexagonal yttrium aluminum perovskite structure, it is also possible that the orthorhombic and hexagonal yttrium aluminum perovskite structure are coexistent.
  • the catalyst or catalyst precursor according to the invention is also possible for the catalyst or catalyst precursor according to the invention to be a material in which the YAG phase as main part, ie preferably greater than 75% by weight, in particular greater than 85% by weight, is used. %, very particularly preferably greater than 95 wt .-% is present, in particular the phase (i) Y3AI5O12 cubic yttrium aluminum Garnet structure.
  • a highly sintered reference sample with the same stoichiometry as the sample to be measured (in terms of the proportion of crystalline phase) is prepared and then set this as the standard sample. The samples to be measured are compared against the standard sample for reference, whereby the reference was previously assigned a value of one hundred percent.
  • the optical analysis method is preferred for nanocrystalline materials if they have very small crystallites whose size is in the range of the wavelength of the incident light.
  • Low coherence lengths are (in diffractometric investigations with an X-ray wavelength of 0.154 nm) in particular when the crystallite sizes are less than 0.5 nm, preferably less than 0.4 and more preferably less than 0.3 nm.
  • Such nanocrystalline materials may be such that they appear as X-ray amorphous in powder diffractometry and as crystalline in UV analysis.
  • all aluminum-containing starting materials can be used as the aluminum source, a preferred aluminum source being selected from the group: pseudo-boehmite, boehmite, gibbsite, bayerite, gamma-alumina, theta-alumina, hydrotalcites, such as magnesium hydrotalcite, colloidal basic aluminas, for example the product " Guifloc "from BK Guilini and other colloidal aluminum sources known to those skilled in the art, as well as mixtures thereof Including, inter alia, the following products from Sasol: Disperal and all types of disperse, Dispal, Pural, Puralox, Catalox, Catapal and also all Pural MG types.
  • the surface structure of the highly reactive alumina or hydroxide source such as theta-alumina, gamma-alumina, pseudo-boehmite, boehmite, gibbsite, bayerite, and mixtures of the foregoing and other highly reactive alumina or hydroxide source could have a significant impact on the formation of an active catalyst.
  • the boehmite used does not consist of dispersible particles, preferably the primary particle size is in the range of less than or equal to 500 nm.
  • dispersible particles means that the particles dispersed in water or slurried particles form a stable dispersion and only after a long time (ie in the range of hours to days) deposited on the bottom of the vessel.
  • the aluminum source is preferably a nanoparticulate aluminum-containing starting material or colloidal primary particles.
  • peptidized aluminum hydroxides, oxide hydrates or oxides can be used as nanoparticulate aluminum-containing starting materials.
  • the peptidization can be carried out by means of organic acids, for example acetic acid, propionic acid, or by means of inorganic acids, for example nitric acid or hydrochloric acid.
  • the colloidal particles can be added by means of stabilizers such as surfactants, soluble polymers or salts, or such stabilizers can be used in the production process.
  • the colloidal primary particles may also consist of partially hydrolyzed alcoholates.
  • shaped bodies of the abovementioned alumina and hydroxide sources which are then brought into contact with the other precursor metal compounds.
  • shaped bodies can be, inter alia, tablets, extrudates or granules or other shaped bodies known to the person skilled in the art.
  • a highly reactive alumina or alumina hydroxide source proves to be particularly advantageous in that it supports the formation of desirable phases.
  • metal compounds those compounds are preferably used which are soluble in solvents or in the temperature range up to 250 ° C are melted and which are inexpensive and available on an industrial scale.
  • the preferred solvents used include the following: water, acidic or alkaline aqueous solutions, alcohols such as methanol, ethanol, propanol, iso-propanol, butanol, ketones such as acetone or methyl ethyl ketone, aromatic solvents such as toluene or xylenes, aliphatic solvents such as cyclohexane or n-hexane, ethers and polyethers such as tetrahydrofuran, di-ethyl ether or di-glyme, esters such as methyl acetate or ethyl acetate.
  • metal compounds are soluble salts, complex compounds or organometallic compounds.
  • salts include nitrates, nitrites, carbonates, halides, acetates, octanoates.
  • complex compounds include EDTA complexes, complexes with amino acid or amines, complexes with polyols or polyacids, complexes with phosphines.
  • organometallic compounds include acetylacetonates, alcoholates, alkyl compounds, compounds with aromatics such as cyclopentadienyl adducts.
  • Metal salts which are not decomposed during the melting or in which the decomposition is kinetically strongly inhibited are preferably used as meltable metal compounds.
  • metal salts examples include nitrates, nitrites, halides, chlorates, bromates, iodates, sulfates, sulfites. Particularly preferred are nitrates, nitrites or salt melts containing nitrates and nitrites.
  • Suitable methods for contacting the metal compounds with the aluminum source include impregnation methods in which the metal compounds are dissolved in a suitable solvent, which are subsequently removed by drying. Such a drying step can be carried out with powdered aluminum source, for example by freeze or spray drying. Alternatively, spray granulation can also be carried out or static drying of the resulting composites can take place. In the context of the invention, in particular the impregnation is a preferred method. It is also possible to use precipitation processes for preparing the catalyst or the catalyst precursor. In this case, all are preferably presented in acidic soluble components in aqueous solution and then precipitated with a basic precipitant.
  • the following are presented in acidic form: aluminum source, yttrium source, possibly a rare earth source, and at least one element from the zinc, copper, nickel, cobalt and iron source.
  • the precipitation is preferably carried out with an aqueous solution of a basic precipitant, specifically above a pH of 7.5.
  • a basic precipitant specifically above a pH of 7.5.
  • the pH and the temperature are controlled in the precipitation and kept constant.
  • organic auxiliary agents to the synthesis system. By means of the organic auxiliary agents, the precipitation process can be influenced so that a particularly finely divided precipitate is formed.
  • Suitable auxiliary agents are, for example, organic acids, complexing agents and / or surface-active agents such as surfactants in ionic or nonionic form and water-soluble polymers. Also included is contacting a basic aluminum-containing solution or dispersion with an acidic solution of all other metal salts which results in precipitation. Such precipitation can be carried out directly after addition, after thermal treatment and / or concentration.
  • kneading or milling an aluminum source in the presence of the yttrium compound and the other metal compounds) with or without the addition of liquids are particularly suitable methods for contacting.
  • the kneading is a preferred method in the context of the invention, since it allows a coupling with a subsequent extrusion and thus may be advantageous for the shaping.
  • metal salts which are preferred for the synthesis and which facilitate the formation of the YAG phase in the presence of zinc, copper, nickel, cobalt and / or iron.
  • rare earth or lanthanides such as lanthanum and cerium.
  • Other cations which are preferred in the invention are those which can be incorporated into the YAG, such as zinc, copper, nickel, cobalt and / or iron.
  • Preferred are, inter alia, magnesium, calcium, gallium, beryllium, chromium, manganese.
  • seed crystals in a preferred embodiment of the process according to the invention, consist of a material with YAG, YAP or YAM phase-the target product-preferably of YAG phase, more preferably of greater than 95% by weight. % YAG phase, more preferably from phase pure YAG.
  • the seed crystals have a small particle size, preferably less than 500 ⁇ m, in particular less than 300 ⁇ m, very particularly preferably less than 100 ⁇ m, with a high specific surface area, preferably greater than 5 m 2 / g, in particular greater than 10 m 2 / g, especially preferably greater than 20 m 2 / g, or consist of agglomerates having a low crystallite size and a high specific surface area.
  • Seed crystals can be prepared from a corresponding YAG material by subjecting it to suitable mechanical and / or chemical treatment, such as grinding in the dry state, milling in the presence of water or milling in the presence of acids or bases.
  • the seed crystals are brought into contact by intensive mixing with the aluminum source.
  • This mixing can be done by milling, kneading, mulling or other methods known in the art.
  • the mixing of the aluminum source with the seed crystals can take place before, during or after contacting with the copper, zinc, cobalt, nickel and / or iron-containing compound and the at least one further metal compound.
  • the alumina source may be provided in the form of a solid, such as powder or granules, and in liquid form. If the alumina source is in liquid form, it is preferred that the aluminum-containing species be dispersed in the solvent or be present therein as colloidal particles.
  • the stability of the colloidal aluminas or else the formation of the colloidal aluminas can be improved by choosing a pH which is either in the range from 2 to 4.5 or in the range from 8 to 14.
  • Suitable agents for preparing or stabilizing the colloidal aluminas are acids such as HNO 3, acetic acid or formic acid or bases such as, for example, aqueous NaOH, KOH or ammonia solution.
  • a colloidal aluminal solution which has peptidized alumina particles and whose pH is in the range from 2 to 4.5.
  • an aluminum solution is used which has one or more basic aluminum sources and whose pH is in the range from 8 to 14.
  • the aluminum source is contacted with at least one metal compound.
  • the addition of the seed crystals can be done before, during or after the addition of the metal compounds. Alternatively, the seed crystals may be added after the drying step.
  • a dispersible nanoparticulate alumina source is used as finely divided powder.
  • the fine Particulate powder consists of primary particles less than or equal to 500 nm, which are present as agglomerates with a D 5 o value of 1 to 100 ⁇ .
  • the aluminum source is contacted in this preferred embodiment with at least one metal compound.
  • the metal compound may be added either as a solution or as a solid. In the case of a solid, a liquid is then added. When adding the solution or the liquid, particular care is taken to ensure that a homogeneous, dough-like mass is produced, which is kneadable and which is distinguished by a very intimate mixing of the alumina source and the metal compound.
  • the addition of the seed crystals can be done before or after the addition of the metal compounds.
  • An essential feature of this preferred embodiment is that the drying (i.e., step (iv)) is preceded by extrusion as a shaping step (i.e., step (vi)).
  • the finely divided powder of the aluminum source is brought into contact with at least one meltable metal compound.
  • the intimate mixing of the alumina source and the reflowable metal compound is carried out at a temperature in the range of 25 ° C to 250 ° C. When choosing the temperature, particular care is taken to ensure that they are above the
  • Melting point of the metal compound is. By melting the metal compound, a particularly homogeneous distribution of the components in the mixture is achieved.
  • the addition of the seed crystals can be done before, during or after the addition of the metal compounds. Alternatively, the seed crystals may also be added only after the mixture has cooled.
  • the cryogenic calcination of the dried mixture or of the molded and dried material obtained after the above-mentioned process steps basically serves to remove the anions from the metal compounds used and to convert them into the corresponding metal oxides.
  • the temperature in the calcination depends on the metal compounds used, preferably the temperature is less than or equal to 550 ° C. and more preferably in the temperature range of 150 ° C. to 550 ° C.
  • the high-temperature calcination of the molded and dried mixture or the low-temperature calcination of the mixture, which was obtained by the above-mentioned process steps, are essential process steps in the preparation of the catalyst according to the invention.
  • the temperature in the high-temperature calcination is preferably greater than or equal to 750 ° C, in particular greater than or equal to 800 ° C, preferably the temperature is greater than or equal to 850 ° C and more preferably the temperature is greater than or equal to 900 ° C.
  • the low-temperature calcination (v) and high-temperature calcination steps (vii) can be carried out in a coherent process step. This is particularly advantageous if the drying step is preceded by a shaping step. If the target temperature of 750 ° C. is undershot during the calcination, a preparation of the catalyst according to the invention could be adversely affected since, if appropriate, the formation of YAG fails or an excessively low proportion of YAG is formed. If a calcining temperature is chosen which is above the suitable temperature range, although phases are formed which have a certain catalytic activity, but the materials have a too small surface area. The upper limit of calcination for the calcining temperature is preferably 1300 ° C, preferably 1250 ° C, and more preferably 1200 ° C.
  • a high specific surface is conducive.
  • materials with surfaces greater than 2 m 2 / g are preferred, particularly preferred are materials with surfaces greater than 4 m 2 / g, very particularly preferably materials with surfaces greater than 8 m 2 / g, very particularly preferred are materials with surface areas greater than 15 m 2 / g.
  • a shaping process is important for the preparation of the catalyst, so that the catalyst can be suitably used in a tubular reactor. This is also related to the fact that the colloidally dissolved aluminum hydroxide or the basic Aluminiumpolychloriddisperison, which is particularly preferably used alumina source, are particularly finely divided and have a high reactivity.
  • a particularly finely divided catalyst material would lead to problems in the technical application. Therefore, it is also particularly advantageous that very finely divided starting components can be used, which then lead with a molding step to special catalysts.
  • the direct introduction of a very finely divided catalyst into a tubular reactor would lead to a high pressure loss or to complete blockage of the reactor, which would affect the catalytic reforming process.
  • the material produced by the process according to the invention can be used in the reforming for the production of synthesis gas in the form of bulk material, pellets or extrudates. be set.
  • the choice of suitable catalyst form depends on the particular process conditions that are important for the production of the synthesis gas.
  • the shaping is carried out according to the invention and preferably according to the process steps (iii) or (v); however, it is also conceivable to carry out the shaping according to process step (vii), although it is not clear whether in all respects all preferred properties of the invention can be achieved if the shaping takes place only after process step (vii).
  • the preparation of a tablet molding is carried out by the steps (x.1) compaction, (x.2) screening and (x.3) tableting.
  • Binder and lubricant can be added to the catalyst material or precursor material used for compaction and tableting.
  • a lubricant for example, graphite or stearic acid can be used.
  • graphite is used.
  • the amount of lubricant is usually not more than 10 wt .-% based on the catalyst material.
  • the target fraction by means of a compaction machine, which makes several steps in a row.
  • the bulk material produced with the compaction machine may possibly have a lower mechanical stability than a material that has been produced with a pressing machine.
  • a shaped body is produced by means of an extrusion step. Such extrusion may be done after step (ii) or step (iii) of the preparation.
  • suspension is dried by means of a spray drier and subsequently subjected to a calcination process.
  • one or more oxides can be added to the catalyst.
  • the formation of certain oxides by special process features or process steps during the synthesis may be controlled to form the binder during the synthesis.
  • Such process features or process steps may include but are not limited to: preferred choice of stoichiometry of the starting compounds, preferred choice of the nature of the starting compounds and especially the source of aluminum, preferred choice of thermal treatment steps.
  • a particularly suitable binder material has a positive effect on the formation of a high surface area of the catalyst according to the invention.
  • Such oxides which form from the binder material during calcination and which are particularly preferred secondary phases include: theta alumina, alpha alumina, yttrium aluminate (YAIO3), yttrium stabilized alumina, yttria stabilized alumina hydroxide.
  • YAIO3 yttrium aluminate
  • yttrium stabilized alumina yttria stabilized alumina hydroxide.
  • a carrier material a ceramic honeycomb body or other shaped body can be used as a carrier material.
  • the stoichiometry of the elements which form the catalyst material is in a certain preferred range.
  • the preferred range of the composition is in each case based on the metallic elements and given on the basis of mole percent. The numbers are to be added to one hundred parts, whereby the presence of oxygen is not taken into account.
  • a yttrium-containing material whose copper, zinc, nickel, iron and / or cobalt content is preferably in the range from 0.01 to 10 mol%, preferably 0.02 to 7 mol, is preferred -%, more preferably 0.1 - 5 mol%.
  • a yttrium-containing material which has at least one further cation species (I) which is selected from the group of rare earths, with rare earths such as Ce, Pr, La, Tb, Nd, Eu being particularly preferred and the content in this at least one cation species is preferably in a range of 0.01 to 10 mol%, more preferably in a range of 0.02 to 8 mol%, and particularly preferably in a range of 0.03 to 5 mol%.
  • a yttrium-containing material which has at least one further cation species (II) which is selected from the group consisting of Mg, Ca, Sr, Ba, Ga, Be, Cr, Mn, the content of which is preferably at least one cation species in a range of 0.01-10 mol%, more preferably in a range of 0.02-8 mol%, and particularly preferably in a range of 0.03-5 mol%.
  • II further cation species
  • the cation species of the rare earths are Ce, Pr and / or La. Particular preference is given to these cation species (I) from the group Ce, Pr and / or La in combination with the cation species (II) from the group Mg and Ga, it being preferred in the invention, when the proportion of cation species is less than 10 mol%, in particular less than 5 mol%, very particularly preferably less than 2 mol%.
  • the catalyst according to the invention is characterized in that it contains an yttrium alumin umgarnet and / or monoclinic yttrium aluminate, in that the catalyst contains yttrium and at least one further element from the group Cu, Zn, Ni, Co, Fe, the yttrium content being in the range of 15 - 80 mol%, preferably 17 - 70 mol% and more preferably in the range of 20 - 70 mol%, the content of the at least one further element from the group Cu, Zn, Ni, Co, Fe in one Range of 0.01-10 mol%, preferably 0.02-7 mol%, more preferably 0.1-5 mol%, the content of Al in a range of 10-90 mol%, preferably 20- 85 mol% and more preferably in the range of 30-80 mol%.
  • the platinum metal-containing embodiments are usually characterized in that the Katalyatormaterialien contain only small amounts of platinum metals. Preference is given to doping with platinum metals based on the oxidic material in the range of 0.1 to 1 percent by weight. Such a doping may take place during the production steps (i) to (v) or (i) to (vi) or in an aftertreatment step.
  • Suitable metal salts are all salts which can be dissolved in a solvent in order thus to obtain as homogeneous a distribution as possible of the metal species the surface of the aluminum source, preferably of boehmite effect.
  • the metal salts added are nitrates or hydrated nitrates. Water is used as the preferred solvent.
  • the aluminum source contains only a small amount of nitrate or is nitrate-free.
  • the nitrate content is preferably less than 40 mol%, more preferably less as 25 mol%, and more preferably smaller than 18 mol%.
  • noble metal-containing salts are added to the impregnating solution as secondary constituents which act as promoters and which lead to an increase in the activity of the catalyst.
  • Preferred precious metals for a promotion include platinum, rhodium, palladium.
  • the amount of the promoters to be used is advantageously less than 5% by weight, preferably less than 2% by weight, very particularly preferably less than 1% by weight.
  • the introduction of the noble metal-containing promoters is to say that they can be supplied during the catalyst synthesis or that they can be deposited on the finished catalyst.
  • the term catalyst precursor describes a material according to the invention that has not yet been subjected to any targeted pretreatment steps (eg described in Technical Catalysis, Jens Hagen, Wiley 1996).
  • the pretreatment takes place in advance of the use of the catalyst material in the context of the method according to the invention, in which the catalyst material is exposed to feed components of the process.
  • Common pretreatment steps are accomplished by exposing the catalyst precursor material to a hydrogen gas stream, a forming gas, as well as other reducing or oxidizing species. In particular, the treatment is carried out at elevated temperatures or hydrothermal conditions; Other pretreatment methods are known in the art and can be used here.
  • the catalyst precursor material is usually present in oxidic form. This means that metallic components - such as copper, nickel, iron, zinc and cobalt - have an oxidation state greater than zero.
  • the term catalyst describes a material which has already been subjected to pretreatment steps.
  • the pretreatment steps involve exposing the catalyst precursor to one or more feed components and / or the final feed gas of the process. At this exposure, the catalyst precursor could convert to the catalyst.
  • Such pretreatment steps to which such a catalyst has been exposed may include, but are not limited to, treatment with hydrogen, forming gas, other reducing or oxidizing agents, particularly at elevated temperatures or hydrothermal conditions, or other pretreatment methods known to those skilled in the art.
  • Such pretreatment methods can be carried out in or outside the reactor.
  • the pretreatment steps should lead to the catalyst being converted into a state favorable for carrying out the reaction. It comes here to a physicochemical changes of the material.
  • Such changes may include: changes in texture, changes in crystallinity, changes in the oxidation states of one or more metals or other elements, formation of metallic nanoparticles, formation of one or more specific catalytically active phases, partial or complete occupancy with organic compounds or coke, complete or partial recrystallization, formation of catalytically active amorphous or partially amorphous surface structures whose composition differs from the bulk material, or other phenomena known to those skilled in the art that may occur upon exposure of a catalyst or catalyst precursor.
  • Such physicochemical transformations described above are typically measurable by analytical methods. In the context of the present invention, however, it is also included that there are no significant differences between catalyst and catalyst precursor or that conversions occur that are not analytically measurable.
  • the fields of application of the catalyst or catalyst precursor according to the invention are extremely versatile and thus the use of the catalyst or the catalyst precursor is particularly suitable for catalytic reforming, for the partial catalytic oxidation of hydrocarbons or hydrocarbon-containing compounds (cPOx), for autothermal reforming (ATR), for dry reforming ( DryRef), for high-temperature carbon dioxide hydrogenation and combined high-temperature carbon dioxide hydrogenation and reforming of hydrocarbons in the presence of methane and in particular for the production of syngas.
  • the Eduktfluidströme advantageously contain at least one gas from the group C0 2 , CO, 0 2 , CH 4 and H 2 0th
  • the invention relates to a process for high-temperature carbon dioxide hydrogenation, for combined high-temperature carbon dioxide hydrogenation and reforming and / or reforming of hydrocarbons, preferably methane, in which the catalyst or the catalyst precursor material according to the invention is used, the process comprising the following steps:
  • the educt gas used in the process is characterized in that it contains more than 40% by volume of hydrogen, carbon dioxide and / or hydrocarbons, preferably methane, preferably more than 50% by volume of hydrogen , Carbon dioxide and / or hydrocarbons, preferably methane, and more preferably more than 70 vol .-% of hydrogen, carbon dioxide and / or hydrocarbons, preferably methane.
  • Other components that are used in the refur- include water and / or circulating gases from the invention or further downstream processes.
  • an activation process is connected upstream of the high-temperature carbon dioxide hydrogenation, the combined high-temperature carbon dioxide hydrogenation and reforming and / or the high-temperature reforming of hydrocarbons.
  • the activation process involves the thermal treatment of the catalyst in a reducing gas atmosphere at a temperature in the range of 300 ° C to 1400 ° C.
  • the catalyst is heated to the process temperature using a controlled heating process.
  • the heating rate is preferably in a range of 1 ° C / min to 30 ° C / min, with a range of 5 ° C / min to 15 ° C / min being preferred.
  • the activation process is coupled with a conditioning of the catalyst;
  • the conditioning is downstream of the activation.
  • Conditioning is a process in which the catalyst is gradually introduced to the process parameters of the target reaction. This is due to the fact that the starting point of the process may require different conditions than for continuous operation. The conditioning steps effectively prevent uncontrolled coking of the catalyst during the so-called start-up.
  • the conditioning of the catalyst consists, for example, in that the catalyst is heated to the process temperature in the presence of carbon dioxide, carbon monoxide, methane, steam and / or hydrogen. It is also possible that the catalyst is conditioned in the presence of water vapor.
  • the educt fluid has a preferred composition in which the proportion of hydrogen, carbon dioxide and hydrocarbons, preferably methane, is greater than 40% by volume, preferably greater than 50% by volume and in particular greater than 70% by volume.
  • the reforming gas may also contain carbon monoxide as a constituent.
  • the reforming gas may also contain oxygen and / or water as constituents.
  • the proportion of O 2 and H 2 O is greater than 5% by volume, preferably greater than 10% by volume and most preferably greater than 20% by volume.
  • the product of the process is a synthesis gas in the composition range hydrogen to carbon monoxide in a volume ratio greater than or equal to one.
  • a preferred ratio of hydrogen to carbon monoxide is in the range of 4 to 0.1 to zero to 1, especially preferably in the range from 3.5: 1 to 0.1: 1, very particularly preferably in the range from 3: 1 to 0.1: 1.
  • the method produces a product gas having a volume fraction of carbon monoxide of more than 90%.
  • hydrogen and the carbon dioxide are present in the educt fluid in a volume ratio greater than or equal to one.
  • a preferred ratio of hydrogen to carbon dioxide is in the range of 5 to 1 to 1 to 1, more preferably in the range of 4.5 to 1 to 1 to 1, most preferably in the range of 4 to 1 to 1 to 1.
  • carbon dioxide and the hydrocarbon-containing starting gas are preferably present in a ratio of greater than 1: 1, particularly preferably greater than 4 to 1, very particularly preferably greater than 5 to 1.
  • the educt fluid can be fed during the process water vapor.
  • the proportion of water vapor in the educt fluid is equal to or less than 30 vol .-%, more preferably equal to or less than 20 vol .-% and even more preferably equal to or less than 15 vol .-%.
  • the reactant gas still standard gases or auxiliary gases can be added.
  • the standard gas is, for example, a rare gas which is added in an amount of 1 to 5 vol.%.
  • the addition of an internal standard in laboratory tests serves to determine the recovery rate.
  • a synthesis gas is produced by means of the process according to the invention which has an H2 / CO ratio which is in the range from 0.85 to 1.4, more preferably the H2 / CO ratio is in a range from 0, 9 to 1, 2, and more preferably in a range of 0.95 to 1, 1.
  • the coke deposit at ⁇ 2 wt .-% carbon content in relation to the catalyst used more preferably ⁇ 1 wt .-%, more preferably ⁇ 0.5 wt%, in particular ⁇ 0.2 wt .-%. Due to the very high thermal stability and the operational stability under pressure at pressures of 5 to 40 bar of the catalyst this can be used over long process times, several thousand hours away.
  • the implementation of reforming at high process pressures, in particular greater than 5 bar, preferably greater than 10 bar, most preferably greater than 20 bar, is advantageous because a synthesis gas is formed, which is also under a very high pressure.
  • the synthesis gas can be used for other processes in which the synthesis gas must be present as a starting material under high pressure.
  • the presence of a high-pressure gas compressor system and compression steps can be saved.
  • the subsequent processes can be methanol synthesis (50-100 bar), Fischer-Tropsch synthesis (40-60 bar) or other gas-to-liquid syntheses. Preferably, these are used by means of the synthesis gas for those subsequent processes in which a h / CO ratio is required, which can also be provided in the context of the inventive method using the yttrium-containing catalysts.
  • Gilufloc 83 (Giulini Co., AI content 12.4% by weight) were weighed into a 600 ml beaker and stirred at room temperature on a magnetic stirrer (50 mm stirring bar, 150 rpm).
  • the mixture was covered and stirred at 80 ° C for 2 h (50 mm stirring bar, 150 rpm). Thereafter, the mixture was transferred to shallow evaporation dishes (Haldenwanger 888-6a / 160mm diameter).
  • the filled dishes were placed in a suitable chamber oven (Nabertherm TH 120/12) and, in a first calcination, nitrate decomposition was carried out under synthetic air (CDA) (6 L / min). All stops were started at 1 K / min and held for one hour (stops 80 ° C, 150 ° C, 200 ° C, 250 ° C, 300 ° C, 350 ° C and 450 ° C). After completion of the last hold time was cooled to room temperature (natural cooling of the furnace).
  • CDA synthetic air
  • the oxydic precursor was now removed from the evaporation bowls and brought to the final grain size (315-500 ⁇ ).
  • the sample with an agate was first through a 1000 ⁇ and then pressed through a 500 ⁇ analysis sieve (Retsch).
  • the fines were then separated from the target fraction by manual sieving (about 10 seconds) using a 315 ⁇ m analytical sieve.
  • the fines were reset as a restoring pattern.
  • the target fraction was calcined again to complete the phase formation.
  • the sample was calcined in an AISint crucible (unglazed AI203 crucible from Haldenwanger) in a muffle furnace (M1 10 from Heraeus) at 900 ° C. (heating ramp 5 K / min) for 4 h under CDA (2 ⁇ m in). After cooling the sample to room temperature, any fines ( ⁇ 315 ⁇ ) formed were separated by re-sieving.
  • the amount of catalyst used was 1 ml, the granulation of the material was 300-500 ⁇ m, the internal diameter of the reactor was 5 mm, and the length of the catalytic test zone was 5 cm.
  • the respective phases with the corresponding gas compositions were started for defined times. These were: Phase I 48 h, Phase II 48 h, Phase III 24 h, Phase IV 24 h, Phase V 24 h and Phase VI 24 h.
  • Table 3 Hydrogen Reaction, Carbon Dioxide Reaction, Methane Yield, and Methane Reaction data of Sample 1-4 compared to the Commercial Reforming Catalyst G1 -85 (BASF) in Phase I to VI
  • Table 4 Carbon content in the active compositions after the screening of catalytically active substances
  • Sample 5 was prepared analogously to Example 1. X-ray diffractometric analysis of the sample revealed a phase-pure Garnet material.
  • the split size of the material to be tested was 0.5-1 ⁇ , the total catalyst volume in the reactor 10 ml, the length of the catalyst zone 8.85 cm, the reactor inner diameter 12mm.
  • the test program is shown in Table 6, 8 phases were started up, the length of the respective test phases I to VIII was 24 hours per phase. At the end of Phase VIII, the catalyst was removed and the carbon content on the catalyst determined.
  • Table 6 Test protocol for the screening of catalytically active substances. For the respective phase, the reaction conditions are given.

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Abstract

L'invention concerne un procédé de fabrication d'un catalyseur pour les procédés à haute température (i) d'hydrogénation du dioxyde de carbone, (ii) d'hydrogénation du dioxyde de carbone à haute température et de reformage combinés et/ou (iii) de reformage des composés contenant des hydrocarbures et/ou du dioxyde de carbone et l'utilisation du catalyseur selon l'invention en combinaison avec le reformage et/ou l'hydrogénation des hydrocarbures, de préférence le méthane et/ou le dioxyde de carbone. La fabrication du catalyseur consiste à mettre en contact une source d'aluminium qui comprend de préférence un précurseur de source hydrosoluble, avec une solution de sel métallique contenant de l'yttrium, à sécher puis à calciner. La solution de sel métallique présente, en plus de l'espèce yttrium, au moins un élément provenant du groupe comprenant le cobalt, le cuivre, le nickel, le fer et le zinc.
PCT/EP2015/055022 2014-03-14 2015-03-11 Catalyseur contenant de l'yttrium pour l'hydrogénation du dioxyde de carbone à haute température, l'hydrogénation du dioxyde de carbone à haute température et le reformage combinés et/ou le reformage ainsi qu'un procédé d'hydrogénation du dioxyde de carbone à haute température, d'hydrogénation du dioxyde de carbone à haute température et de reformage combinés et/ou de reformage WO2015135968A1 (fr)

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RU2016140372A RU2016140372A (ru) 2014-03-14 2015-03-11 Содержащий иттрий катализатор для высокотемпературного гидрирования диоксида углерода, для комбинированного высокотемпературного гидрирования диоксида углерода и риформинга и/или для риформинга, а также способ высокотемпературного гидрирования диоксида углерода, комбинированного высокотемпературного гидрирования диоксида углерода и риформинга и/или риформинга
JP2016557232A JP2017507779A (ja) 2014-03-14 2015-03-11 高温二酸化炭素水和、高温二酸化炭素水和および改質の組合せ、ならびに／または改質のためのイットリウム含有触媒、ならびに高温二酸化炭素水和、高温二酸化炭素水和および改質の組合せ、ならびに／または改質のための方法
KR1020167028074A KR20160133490A (ko) 2014-03-14 2015-03-11 고온 이산화탄소 수소화, 조합된 고온 이산화탄소 수소화 및 개질, 및/또는 개질을 위한 이트륨 함유 촉매, 및 고온 이산화탄소 수소화, 조합된 고온 이산화탄소 수소화 및 개질, 및/또는 개질을 위한 방법
CN201580013170.6A CN106102905A (zh) 2014-03-14 2015-03-11 用于高温二氧化碳氢化、用于组合高温二氧化碳氢化和重整和/或用于重整的含钇催化剂，和用于高温二氧化碳氢化，用于组合高温二氧化碳氢化和重整和/或用于重整的方法
US15/126,217 US20170080407A1 (en) 2014-03-14 2015-03-11 Yttrium-containing catalyst for high-temperature carbon dioxide hydration, combined high-temperature carbon dioxide hydration, and reforming and/or reforming, and a method for high-temperature carbon dioxide hydration, combined high-temperature carbon dioxide hydration and reforming and/or reforming
EP15708833.7A EP3116826B1 (fr) 2014-03-14 2015-03-11 Catalysezr contenant de l'yttrium pour la hydrogenation de dioxid de carbone, hydrogenation de dioxid de carbone a haute temperature et/ou reformage et procede pour la hydrogenation de dioxid de carbone et/ou reformage
CA2942587A CA2942587A1 (fr) 2014-03-14 2015-03-11 Catalyseur renfermant de l'yttrium destine a l'hydratation de dioxyde de carbone haute temperature, l'hydratation de dioxyde de carbone haute temperature combinee et le reformage et/ou le reformage, et une methode d'hydratation de dioxyde de carbone haute temperature, d'hydratation de dioxyde de carbone haute temperature et de reformage et/ou de reformage

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WO2018219986A1 (fr) 2017-06-02 2018-12-06 Basf Se Procédé d'hydrogénation de dioxyde de carbone en présence d'un catalyseur contenant de l'iridium et/ou du rhodium
WO2018219992A1 (fr) 2017-06-02 2018-12-06 Basf Se Procédé d'hydrogénation de dioxyde de carbone en présence d'un catalyseur contenant du nickel et des spinelles de magnésium
EP3770145A1 (fr) 2019-07-24 2021-01-27 Basf Se Processus de production continue soit d'acroléine soit d'acide acrylique comme produit cible à partir de propène
WO2024003347A1 (fr) 2022-07-01 2024-01-04 Basf Se Catalyseur à base de cobalt et de strontium pour la conversion d'hydrocarbures en gaz de synthèse
WO2024003354A1 (fr) 2022-07-01 2024-01-04 Basf Se Catalyseur à base de cobalt pour la conversion d'hydrocarbures en gaz de synthèse

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EP3371161A1 (fr) 2015-11-04 2018-09-12 Basf Se Procédé pour la préparation d'acide furan-2,5-dicarboxylique
CA3003764A1 (fr) 2015-11-04 2017-05-11 Basf Se Procede pour la preparation d'un melange comprenant du 5-(hydroxymethyl)furfural et des esters specifiques du hmf
CN107597199A (zh) * 2017-09-13 2018-01-19 武汉凯迪工程技术研究总院有限公司 循环流化床烃重整催化剂及其制备方法和应用
WO2020012687A1 (fr) * 2018-07-09 2020-01-16 株式会社村田製作所 Catalyseur de reformage d'hydrocarbures et appareil de reformage d'hydrocarbures
AU2019393943B2 (en) 2018-12-03 2022-03-17 Shell Internationale Research Maatschappij B.V. A process and reactor for converting carbon dioxide into carbon monoxide
US11987503B2 (en) * 2019-04-26 2024-05-21 Nippon Yttrium Co., Ltd. Powder for film formation or sintering
CN112174215B (zh) * 2019-07-01 2021-11-26 中国科学院大连化学物理研究所 一种耐高温氧载体和制备及其应用
KR102359490B1 (ko) 2019-11-14 2022-02-08 전남대학교산학협력단 이산화탄소환원촉매, 상기 환원촉매 제조방법 및 상기 환원촉매를 이용한 탄화수소화합물 제조방법
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WO2018219986A1 (fr) 2017-06-02 2018-12-06 Basf Se Procédé d'hydrogénation de dioxyde de carbone en présence d'un catalyseur contenant de l'iridium et/ou du rhodium
WO2018219992A1 (fr) 2017-06-02 2018-12-06 Basf Se Procédé d'hydrogénation de dioxyde de carbone en présence d'un catalyseur contenant du nickel et des spinelles de magnésium
EP3770145A1 (fr) 2019-07-24 2021-01-27 Basf Se Processus de production continue soit d'acroléine soit d'acide acrylique comme produit cible à partir de propène
WO2021013640A1 (fr) 2019-07-24 2021-01-28 Basf Se Procédé de production continue d'acroléine ou d'acide acrylique en tant que produit cible à partir de propène
WO2024003347A1 (fr) 2022-07-01 2024-01-04 Basf Se Catalyseur à base de cobalt et de strontium pour la conversion d'hydrocarbures en gaz de synthèse
WO2024003354A1 (fr) 2022-07-01 2024-01-04 Basf Se Catalyseur à base de cobalt pour la conversion d'hydrocarbures en gaz de synthèse

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JP2017507779A (ja) 2017-03-23
TW201600170A (zh) 2016-01-01
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RU2016140372A (ru) 2018-04-16
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CA2942587A1 (fr) 2015-09-17

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